System and method for purifying depleted brine

ABSTRACT

A system and method for removing impurities to reconstitute a NaCl stream to a saturated solution salt solution and remove any impurities such as sodium bisulfite (NaHSO 3 ), sodium chlorate (NaClO 3 ) and sodium iodide (NaI) to improve brine quality from an electrolytic cell is disclosed, including an evaporation system connected to the electrolytic cell, a brine treatment system connected to the evaporation system and the electrolytic cell. A waste treatment system is connected to the evaporation system. The evaporation system includes a set of evaporators that concentrates the brine. Sodium chloride is precipitated from the set of evaporators to the brine treatment system. Impurities are precipitated from the set of evaporators. The brine treatment system includes a hydrocyclone and a centrifuge that separates sodium chloride from water. The sodium chloride is mixed with water to create a concentrated and purified brine.

CROSS REFERENCE TO RELATED APPLICATION

This application is a continuation of U.S. patent application Ser. No.14/959,493 which filed Dec. 4, 2015, now U.S. Pat. No. 10,227,702, whichclaims the benefit of U.S. Provisional Patent Application No. 62/088,152filed on Dec. 5, 2014. Each patent application identified above isincorporated herein by reference in its entirety to provide continuityof disclosure.

FIELD OF THE INVENTION

The present invention relates to the treatment of waste streams. Inparticular, the present invention relates to treating depleted brinefrom a chlor-alkali processing system.

BACKGROUND OF THE INVENTION

Chlor-alkali systems and processes produce chlorine, sodium hydroxide(caustic soda) and other caustic alkali products. Typically, the processis conducted in an electrolytic membrane cell using a brine, which is anaqueous solution of sodium chloride. The brine is fed into theelectrolytic cell, which includes an anode side and a cathode sideseparated by a membrane. A current is passed through the electrolyticcell. As a result, the sodium chloride brine splits into its constituentparts. The membrane allows sodium ions to pass through it to the cathodeside, where it forms sodium hydroxide in a solution. The membrane allowsonly positive sodium ions to pass through to prevent the chlorine frommixing with the sodium hydroxide. The chloride ions are oxidized tochlorine gas at the anode. Hydrogen gas and hydroxide ions are formed atthe cathode. After this process, the brine is depleted and cannot beused in the electrolytic cell. Therefore, the depleted brine must betreated or replaced with fresh brine in order for the membraneelectrolytic cell to properly operate. Further, the depleted brine mustbe purified to remove impurities that may cause fouling of the membrane.

The prior art has attempted to address the need for purified brine withlimited success. For example, U.S. Pat. No. 4,169,773 to Lai, et al.discloses a system and method for the electrolytic production of alkalimetal hydroxide and halide with acidification of part of a recirculatinganolyte stream to remove halite. The system in Lai diverts a brinestream from a membrane cell to a reaction vessel for treatment. In thereaction vessel, concentrated hydrochloric acid (HCl) is added to thebrine stream to minimize chlorine dioxide production. The treated streamis then irradiated with ultra violet light. The irradiated stream ispassed through a scrubber before being reintroduced to the membranecell. However, the system in Lai requires the use of hydrochloric acidand an irradiation step that increases costs and inefficiencies.

U.S. Pat. No. 6,309,530 to Rutherford, et al. discloses a system andmethod for the concentration of depleted brine exiting a chlor-alkalimembrane cell plant. The depleted brine flows from a membrane cell intoa dechlorinator where chemicals, such as sodium carbonate and sodiumhydroxide are added. The dechlorinated brine is fed into a concentratorsystem where water vapor is removed. The reconcentrated brine is thenready for use. However, like Lai, the system in Rutherford requires theaddition of chemicals, thereby leading increased costs.

Therefore, there is a need in art for a system and method for purifyingbrine that does not add chemicals to the brine and does not requirecostly compression and/or condensation steps. Thus, there is a need fora system and method of purifying depleted brine with minimal costs andsteps to treat the depleted brine.

SUMMARY

In a preferred embodiment, a system and method for concentrating andpurifying depleted brine from an electrolytic cell is disclosed. Thesystem includes a reconstitution/evaporation system connected to theelectrolytic cell, a brine treatment system connected to thereconstitution/evaporation system and the electrolytic cell. A wastetreatment system is connected to the reconstitution/evaporation system.

The reconstitution/evaporation system further includes a set of effectevaporators that evaporates water vapor from the depleted brine toconcentrate the brine. Sodium chloride is precipitated from the set ofeffect evaporators to the brine treatment system. Impurities such assodium bisulfite (NaHSO₃), sodium chlorate (NaClO₃) and sodium iodide(NaI) are precipitated from the set of effect evaporators, to improvebrine quality.

The brine treatment system includes a hydrocyclone and a centrifuge thatseparates sodium chloride from water. The sodium chloride is mixed withwater to create a concentrated and purified brine. The brine is storedfor later use.

The waste treatment system includes a waste treatment tank that receiveswaste water from the set of effect evaporators. The waste water includesthe removed impurities such as sodium bisulfite (NaHSO₃), sodiumchlorate (NaClO₃) and sodium iodide (NaI). Each of the pH level and thechlorine level of the waste water is adjusted to predetermined levels.The waste water is passed through a carbon filter to complete thetreatment process.

BRIEF DESCRIPTION OF THE DRAWINGS

In the detailed description presented below, reference is made to theaccompanying drawings.

FIG. 1 is a general schematic drawing of a system for treating depletedbrine of a preferred embodiment.

FIG. 2 is a schematic drawing of a system for treating depleted brine ofa preferred embodiment.

FIG. 3 is a schematic drawing of a reconstitution/evaporation system ofa preferred embodiment.

FIG. 4 is a schematic drawing of a brine treatment system of a preferredembodiment.

FIG. 5 is a schematic drawing of a waste water treatment system of apreferred embodiment.

DETAILED DESCRIPTION

Referring to FIG. 1, a general schematic of system 100 for treatingdepleted brine will be described. System 100 is connected electrolyticcell 101. System 100 includes reconstitution/evaporation system 102connected to electrolytic cell 101, brine treatment system 103 connectedto reconstitution/evaporation system 102 and to electrolytic cell 101.Raw brine supply 106 is connected to brine treatment system 103. Wastetreatment system 104 is connected to reconstitution/evaporation system102 for the output of waste 105. Catholyte 108 and hydrogen and chloridegases 110 are remaining outputs from electrolytic cell 101.

Referring to FIG. 2, system 200 is connected to electrolytic cell 201and forms a crystallizer which purifies depleted brine for reuse.Electrolytic cell 201 includes an anode side and a cathode sideseparated by a membrane. Each of water stream 202 and brine stream 203is connected to the anode side and flows into electrolytic cell 201. Anelectric current is supplied to electrolytic cell 201. Each of Catholytestream 207 and hydrogen stream 205 is connected to and flows from thecathode side of electrolytic cell 201. Each of lean brine stream 206 andchlorine stream 204 is connected to and flows from the anode side ofelectrolytic cell 201. Lean brine stream 206 flows into brine evaporatorfeed tank 208 at a rate from approximately 2,800 gallons per minute(gpm) to 3,200 gpm. Lean brine stream 206 is also connected to leanbrine line 253

System 200 includes brine evaporator feed tank 208, which is connectedto a set of effect evaporators. Brine evaporator feed tank 208 isconnected first effect evaporator 210 with depleted brine line 209.Depleted brine line 252 is connected to depleted brine line 209 and tosalt dissolving tank 224. Depleted brine line 209 and depleted brineline 252 have a flow rate of approximately 2,800 gpm to 3,200 gpm and aniodine level of approximately 0.13 ppm to 0.17 ppm. Lean brine line 253is also connected to salt dissolving tank 224. First effect evaporator210 is connected to steam supply 211 and to cooled steam line 243.Second effect evaporator 212 is connected to first effect evaporator 210with vapor line 228 and liquid line 229. Second effect evaporator 212 isfurther connected to cooled vapor line 244. Second effect evaporator 212is connected to third effect evaporator 213 with vapor line 230 andliquid line 231. Third effect evaporator 213 is connected to fourtheffect evaporator 214 with vapor line 232 and to fifth effect evaporator215 with liquid line 233. Third effect evaporator 213 is furtherconnected to cooled vapor line 245. Fourth effect evaporator 214 isfurther connected to fifth effect evaporator 215 with vapor line 234 andliquid line 235. Fourth effect evaporator is further connected toprecipitates outlet 216, cooled vapor line 247, and to waste watertreatment tank 217 with waste line 236. Waste water treatment tank 217is connected to treatment inlet 218 and to water outlet 219. Waste watertreatment tank 217 includes carbon filter 227 adjacent to water outlet219.

Third effect evaporator 213 is further connected to hydrocyclone 220with precipitate line 237. Hydrocyclone 220 is connected to waste wateroutlet 221 to waste water treatment tank 217.

In one embodiment, hydrocyclone 220 is connected to centrifuge 222 withcentrifuge line 238. In this embodiment, centrifuge 222 is connected towaste water outlet 223 to waste water treatment tank 217 and to saltdissolving tank 224 with solids line 239.

In another embodiment without the centrifuge, hydrocyclone 220 isconnected to salt dissolving tank 224.

Fifth effect evaporator 215 is further connected to salt dissolving tank224 with solids line 240, water vapor outlet 226, and to cooled vaporline 246. Salt dissolving tank 224 is further connected to raw brinetank 225 with brine line 241. Feed line 249 is connected to raw brinetank 225. Raw brine tank 225 is connected to brine treatment 251 withbrine supply line 242. Brine treatment 251 is connected to electrolyticcell 201 with brine stream 203.

In a preferred embodiment, each of first effect evaporator 210, secondeffect evaporator 212, third effect evaporator 213, fourth effectevaporator 214, and fifth effect evaporator 215 is a falling film effectevaporator. Other suitable evaporators known in the art may be employed.

In one embodiment, any of first effect evaporator 210, second effectevaporator 212, third effect evaporator 213, fourth effect evaporator214, and fifth effect evaporator 215 includes a recirculation line.

In a preferred embodiment, hydrocyclone 220 is a stainless steelhydrocyclone manufactured by ChemIndustrial Systems, Inc. of Cedarburg,Wis. Other suitable hydrocyclone separators known in the art may beemployed.

In a preferred embodiment, centrifuge 222 is a disc-stack centrifuge.Other suitable centrifuges known in the art may be employed.

In one embodiment, steam supply 211 is a multiple effect evaporator(MEE) steam driver. Any steam driver known in the art may be employed.

In another embodiment, steam supply 211 is a mechanical vaporrecompressor (MVR) power driver. Any power driver known in the art maybe employed.

In a preferred embodiment, brine treatment 251 is a clarifier to removeany sludge in the brine prior to introduction into electrolytic cell201. Other types of solids separation known in the art may be employed.

It will be appreciated by those skilled in the art that any type ofsuitable piping means may be employed to connect the previouslydescribed vessels including the effect evaporators, tanks, hydrocyclone,centrifuge, and brine treatment. It will be further appreciated that anysuitable directing devices including pumps, valves, sensors,controllers, supervisory control and data acquisition (“SCADA”) systemand software may be employed to direct steam, a liquid stream, a vaporstream and/or solids into and/or out of any of the previously describedvessels.

In other embodiments, any number of holding tanks may be connectedadjacent to any of effect evaporators 210, 212, 213, 214, and 215.

In other embodiments, any number of heat exchangers may be connected toany of effect evaporators 210, 212, 213, 214, and 215 to provideadditional heating or cooling to the effect evaporators.

Referring to FIG. 3, a preferred use of reconstitution/evaporationsystem 300 will now be described. In a preferred embodiment,approximately 40% to 50% of the depleted brine stored in brineevaporator feed tank 301 is sent to first effect evaporator 303 asdepleted brine stream 302. Each of depleted brine streams 302 and 330are sent at a rate of approximately 2,800 gpm to 3,200 gpm. Each ofdepleted brine streams 302 and 330 has a concentration level ofapproximately 1% to 3% NaCl and an iodine level of approximately 0.13parts per million (ppm) to 0.17 ppm. Each of the concentration levels ofthe liquid streams as used in this application is defined as apercentage of the total weight. Steam 304 is introduced into firsteffect evaporator 303 at a rate of approximately 17,000 pounds per hour(lbm/hr) to 24,000 lbm/hr to heat depleted brine stream 302 to anoperating temperature of approximately 230° F. to 244° F. for a time ofapproximately 12 minutes to 18 minutes. First effect evaporator 303 hasan operating pressure of approximately 5 psig to 9 psig. Cooled steam325 is produced by steam 304 heating depleted brine stream 302. Cooledsteam 325 is directed out of first effect evaporator 303 at a rate ofapproximately 19,000 lbm/hr to 23,000 lbm/hr. Water vapor 305 isevaporated from depleted brine stream 302 in first effect evaporator 303to create liquid stream 306. Water vapor 305 is directed from firsteffect evaporator 303 into second effect evaporator 307 at a rate fromapproximately 20,000 lbm/hr to 22,000 lbm/hr. Water vapor 305 has atemperature in a range from approximately 240° F. to 245° F. Liquidstream 306 is directed from first effect evaporator 303 into secondeffect evaporator 307 at a rate from approximately 2,800 gpm to 3,200gpm. Liquid stream 306 has a concentration level of approximately 10% to14% NaCl and an iodine level of approximately 0.20 ppm to 0.24 ppm.

In a preferred embodiment, the levels and concentrations are measuredwith a spectrophotometer, such as an Agilent Cary-60 UV-Visspectrophotometer manufactured by Agilent Technologies. The iodinelevels are measured in accordance with ASTM D3869-09 (Standard TestMethods for Iodide and Bromide Ions in Brackish Water, Seawater, andBrines by the International Association for Testing and Materials (ASTMInternational)) wherein a 25 milliliter (ml) brine sample undergoesbuffering to a slightly acidic state, along with subsequent treatmentwith bromine solution, sodium formate, potassium iodide, and a starchindicator. The treated sample is then read on the spectrophotometer, ata wavelength of 570 nanometers (nm), to determine concentration.

In one embodiment, cooled steam 325 is reheated and recirculated assteam 304. Any heating and recirculating means known in the art may beemployed.

Water vapor 305 heats liquid stream 306 in second effect evaporator 307to an operating temperature of approximately 210° F. to 214° F. for atime of approximately 12 minutes to 18 minutes. Cooled water vapor 326is produced from water vapor 305 heating liquid stream 306. Cooled watervapor 326 is directed out of second effect evaporator 307 at a rate fromapproximately 20,000 lbm/hr to 22,000 lbm/hr. Second effect evaporator307 has an operating pressure of approximately −2 psig to 2 psig. Watervapor 309 is evaporated from liquid stream 306 in second effectevaporator 307 to create liquid stream 308. Water vapor 309 is directedfrom second effect evaporator 307 into third effect evaporator 310 at arate from approximately 20,000 lbm/hr to 22,000 lbm/hr. Water vapor 309has a temperature in a range from approximately 240° F. to 245° F.Liquid stream 308 is directed from second effect evaporator 307 intothird effect evaporator 310 at a rate from approximately 2,800 gpm to3,200 gpm. Liquid stream 308 has a concentration level of approximately15% to 19% NaCl.

Water vapor 309 heats liquid stream 308 in third effect evaporator 310to an operating temperature of approximately 210° F. to 214° F. for atime of approximately 12 minutes to 18 minutes. Cooled water vapor 327is produced from water vapor 309 heating liquid stream 308. Cooled watervapor 327 is directed out of third effect evaporator 310 at a rate fromapproximately 20,000 lbm/hr to 22,000 lbm/hr. Third effect evaporator310 has an operating pressure of approximately −2 psig and 2 psig. Watervapor 319 is evaporated from liquid stream 308 in third effectevaporator 310 to create liquid stream 312. Liquid stream 312 has aconcentration level of NaCl above saturation. Sodium chloride 311 isprecipitated from third effect evaporator 310 at a rate fromapproximately 8,000 lbm/hr to 9,000 lbm/hr into brine treatment system323, as will be further described below. The concentration level ofliquid stream 312 is reduced to approximately 19% to 23% NaCl.

Water vapor 319 is directed from third effect evaporator 310 into fourtheffect evaporator 314 at a rate from approximately 20,000 lbm/hr to22,000 lbm/hr. Water vapor 319 has a temperature in a range fromapproximately 240° F. to 245° F. Liquid stream 312 is directed fromthird effect evaporator 310 into fifth effect evaporator 313 at a ratefrom approximately 2,800 gpm to 3,200 gpm.

Water vapor 315 from fourth effect evaporator 314 is directed into fiftheffect evaporator 313 at a rate from approximately 20,000 lbm/hr to22,000 lbm/hr to heat liquid stream 312 in fifth effect evaporator 313to an operating temperature of approximately 105° F. to 115° F. for atime of approximately 12 minutes to 18 minutes. Cooled water vapor 328is produced from water vapor 315 heating liquid stream 312. Cooled watervapor 328 is directed out of fifth effect evaporator 313 at a rate fromapproximately 20,000 lbm/hr to 22,000 lbm/hr. Fifth effect evaporator313 has an operating pressure of approximately −16 psig to −12 psig.Water vapor 317 is evaporated from liquid stream 312 in fifth effectevaporator 313 to create liquid stream 316. Liquid stream 316 has aconcentration level of NaCl above saturation. Sodium chloride 318 isprecipitated from fifth effect evaporator 313 at a rate fromapproximately 8,000 lbm/hr to 9,000 lbm/hr into brine treatment system323, as will be further described below. The concentration level ofliquid stream 316 is reduced to approximately 18% to 24% NaCl.

Water vapor 317 is directed out of fifth effect evaporator 313 at a ratefrom approximately 20,000 lbm/hr to 22,000 lbm/hr. Liquid stream 316 isdirected from fifth effect evaporator 313 into fourth effect evaporator314 at a rate from approximately 2,800 gpm to 3,200 gpm.

Water vapor 319 from third effect evaporator 310 is directed into fourtheffect evaporator 314 at a rate from approximately 20,000 lbm/hr to22,000 lbm/hr and heats liquid stream 316 in fourth effect evaporator314 to an operating temperature of approximately 210° F. to 214° F. fora time of approximately 12 minutes to 18 minutes. Cooled water vapor 329is produced from water vapor 319 heating liquid stream 316. Cooled watervapor 329 is directed out of fourth effect evaporator 314 at rate fromapproximately 20,000 lbm/hr to 22,000 lbm/hr. Fourth effect evaporator314 has an operating pressure of approximately −2 psig to 2 psig. Watervapor 315 is evaporated from liquid stream 316 in fourth effectevaporator 314 to form waste water 322. Waste water 322 has aconcentration level of NaCl above saturation. Sodium sulfate (NaSO₄) 320and sodium chloride 321 precipitate from waste stream 322 in fourtheffect evaporator 314 at a rate of approximately 7,000 lbm/hr to 9,000lbm/hr. Waste water 322 then has a concentration level of approximately17% to 21% NaCl. Waste water 322 is directed from fourth effectevaporator 314 at a rate of approximately 2,500 gpm to 3,500 gpm intowaste treatment system 324, as will be further described below.

In one embodiment, cooled water vapors 326, 327, 328, and 329 arecombined with water vapor 317 and condensed for use as a water supply.Any type of condensation means known in the art may be employed.

Referring to FIG. 4, brine treatment system 400 will now be furtherdescribed. Sodium chloride 401 is directed from third effect evaporator413 into hydrocyclone 402 at a rate from approximately 8,000 lbm/hr to9,000 lbm/hr. Hydrocyclone 402 has a feed pressure of approximately 45psi to 55 psi and a split ratio of approximately 82/18 to 78/22, heavies(solids) to lights (liquids). Hydrocyclone 402 spins sodium chloride 401to separate waste water 403 from sodium chloride 404.

In one embodiment, sodium chloride 404 is directed from hydrocyclone 402into centrifuge 405 at a rate from approximately 8,000 lbm/hr to 9,000lbm/hr. Centrifuge 405 spins sodium chloride 404 to further separatesodium chloride 407 from waste water 406. Centrifuge 405 spins at a rateof approximately 9,000 rpm to 11,000 rpm. Sodium chloride 407 is now ina purified crystallized form.

In another embodiment, sodium chloride 404 is directed into saltdissolving tank 408 at a rate from approximately 8,000 lbm/hr to 9,000lbm/hr.

Sodium chloride 407 is directed from centrifuge 405 into salt dissolvingtank 408 at a rate from approximately 8,000 lbm/hr to 9,000 lbm/hr.Sodium chloride 409 is directed from fifth effect evaporator 414 intosalt dissolving tank 408 at a rate from approximately 8,000 lbm/hr to9,000 lbm/hr. Lean brine 416 having a concentration level ofapproximately 1% to 3% NaCl is directed into salt dissolving tank 408 ata rate from approximately 2,800 gpm to 3,200 gpm. Depleted brine 422having a concentration level of approximately 1% to 3% NaCl is directedinto salt dissolving tank 408 at a rate from approximately 2,800 gpm to3,200 gpm. Sodium chloride 407 is mixed with sodium chloride 409,depleted brine 422, and lean brine 416 in salt dissolving tank 408 for atime of approximately 12 minutes to 18 minutes to form concentratedbrine 410. Concentrated brine 410 has a concentration level ofapproximately 19% to 23% NaCl. Concentrated brine 410 is sent from saltdissolving tank 408 into raw brine tank 411 for storage. Raw brine 419having a concentration level of approximately 19% to 23% NaCl isdirected into raw brine tank 411 at a rate from approximately 2,800 gpmto 3,200 gpm. Untreated brine 420 having a concentration level ofapproximately 19% to 23% NaCl is directed from raw brine tank 411 tobrine treatment 417 at a rate from approximately 2,800 gpm to 3,200 gpmto remove sludge. Brine supply 412 having a concentration level ofapproximately 19% to 23% NaCl is directed into electrolytic cell 415,which is connected to reconstitution/evaporation system 418, at a ratefrom approximately 2,800 gpm to 3,200 gpm.

Referring to FIG. 5, waste treatment system 500 will now be furtherdescribed. Waste water 502 is directed from a fourth effect evaporatorinto waste water treatment tank 501 at a rate of approximately 2,500 gpmto 3,500 gpm. Waste water 502 includes sodium chlorate (NaClO₃) andsodium iodide (NaI) having concentration levels of approximately 4% to6% and approximately 6% to 8%, respectively. In waste water treatmenttank 501, the pH level of waste water 502 is adjusted to be in a pHrange of approximately 6 to 7. Any suitable means for adjusting the pHlevel known in the art may be employed. A chlorine level of waste water502 is measured. If the chlorine level exceeds 4 ppm, then sodiumbisulfite (NaHSO₃) 503 is added to waste water 502 to lower the chlorinelevel. Waste water 502 is passed through a carbon filter to form treatedwater 504, which is sent to a plant outfall at a rate of approximately2,500 gpm to 3,000 gpm.

It will be appreciated by those skilled in the art that changes could bemade to the embodiments described above without departing from the broadinventive concept. It is understood, therefore, that this disclosure isnot limited to the particular embodiments herein, but it is intended tocover modifications within the spirit and scope of the presentdisclosure as defined by the appended claims.

1. In a system for creating a concentrated brine from a depleted brinecomprising a set of effect evaporators, a hydrocyclone connected to theset of evaporators, a salt dissolving tank connected to the set ofeffect evaporators and the hydrocyclone, and a waste system connected tothe set of effect evaporators, a method comprising the steps of:receiving the depleted brine into the set of effect evaporators;receiving steam into the set of effect evaporators; creating a set ofliquid streams in the set of effect evaporators from the depleted brineand the steam; removing a precipitate from the set of liquid streams;separating a first solids from the precipitate; removing a second solidsfrom the set of liquid streams; and, creating the concentrated brinefrom the first solids and the second solids.
 2. The method of claim 1,wherein removing waste further comprises the steps of: creating a wasteline from the set of liquid streams; removing a waste water from thewaste line; and, creating a treated water from the waste water.
 3. Themethod of claim 1, wherein the step of creating a set of liquid streamsfurther comprises the steps of: evaporating a set of water vapors fromthe set of liquid streams; and, removing a set of cooled water vaporsfrom the set of effect evaporators.
 4. The method of claim 3, whereinthe step of evaporating a set of water vapors from the set of liquidstreams further comprises the steps of: heating the depleted brine withthe steam to create the set of water vapors; and, heating the set ofliquid streams with the set of water vapors.
 5. The method of claim 1,further comprising the step of pressurizing the set of evaporators in apressure range from about −14 psig to about 7 psig.
 6. The method ofclaim 1, wherein the step of creating a set of liquid streams furthercomprises the step of concentrating the set of liquid streams fromapproximately 2% NaCl to approximately 21% NaCl.
 7. The method of claim1, wherein the step of creating the set of liquid streams furthercomprises the step of heating the set of liquid streams in a temperaturerange from about 110° F. to about 237° F.
 8. A system for creating aconcentrated brine from a depleted brine comprising: a set ofevaporators; a hydrocyclone connected to the set of evaporators; acentrifuge connected to the hydrocyclone; a salt dissolving tankconnected to the set of evaporators, the hydrocyclone, and thecentrifuge; a waste system connected to the set of evaporators; wherebythe depleted brine is directed through the set of evaporators to createthe concentrated brine in the salt dissolving tank.
 9. The system ofclaim 8, wherein the set of evaporators further comprises: a firstevaporator; a second evaporator connected to the first evaporator; athird evaporator connected to the second evaporator; a fourth evaporatorconnected to the third evaporator; and, a fifth evaporator connected tothe third evaporator and the fourth evaporator.
 10. The system of claim9, wherein the hydrocyclone is connected to the third evaporator, andwherein the system further comprises a first precipitate directed fromthe third evaporator to the hydrocyclone.
 11. The system of claim 10,wherein the salt dissolving tank is connected to the fifth evaporator,and wherein the system further comprises a second precipitate directedfrom the fifth evaporator to the salt dissolving tank.
 12. The system ofclaim 11, further comprising a brine inlet for introducing a lean brine,connected to the salt dissolving tank, and wherein the concentratedbrine is created from the first precipitate, the second precipitate, andthe lean brine.
 13. The system of claim 9, further comprising: a wastestream created by the fourth evaporator; and, a set of wasteprecipitates created by the fourth evaporator.
 14. The system of claim8, further comprising: a raw brine tank connected to the salt dissolvingtank; and, a brine treatment connected to the raw brine tank.
 15. Asystem for creating a concentrated brine from a depleted brinecomprising: a first evaporator connected to a second evaporator; thesecond evaporator connected to a third evaporator; the third evaporatorconnected to a fourth evaporator, a fifth evaporator, and ahydrocyclone; the hydrocyclone connected to a centrifuge; the fifthevaporator and the centrifuge connected a salt dissolving tank; thefourth evaporator connected to a waste system; a steam source and adepleted brine source connected to the first evaporator, whereby a firstliquid stream and a first water vapor are created through evaporation;the first liquid stream and the first water vapor supplied to the secondevaporator, whereby a second liquid stream and a second water vapor arecreated through evaporation; the second liquid stream and the secondwater vapor supplied to the third evaporator, whereby a third liquidstream, a third water vapor, and a precipitate are created throughevaporation; the precipitate supplied to the hydrocyclone, whereby afirst solids is created through separation; the first solids supplied tothe centrifuge, whereby a second solids is created through separation;the third liquid stream and a fourth water vapor supplied to the fifthevaporator, whereby a fourth liquid stream and a third solids arecreated through evaporation; the fourth liquid stream and the thirdwater vapor supplied to the fourth evaporator, whereby a waste liquidstream and the fourth water vapor are created through evaporation; and,the second solids and the third solids supplied to the salt dissolvingtank; whereby a concentrated brine is created.
 16. The system of claim15, wherein the first evaporator operates at approximately 7 psig. 17.The system of claim 15, wherein the second evaporator operates atapproximately 0 psig.
 18. The system of claim 15, wherein the thirdevaporator operates at approximately 0 psig.
 19. The system of claim 15,wherein the fifth evaporator operates at approximately −14 psig.
 20. Thesystem of claim 15, wherein: the fourth evaporator operates atapproximately 0 psig; and, the waste liquid stream supplied to the wastesystem.